WO2014154761A1 - Dispositif de filtration et d'émulsification - Google Patents

Dispositif de filtration et d'émulsification Download PDF

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Publication number
WO2014154761A1
WO2014154761A1 PCT/EP2014/056080 EP2014056080W WO2014154761A1 WO 2014154761 A1 WO2014154761 A1 WO 2014154761A1 EP 2014056080 W EP2014056080 W EP 2014056080W WO 2014154761 A1 WO2014154761 A1 WO 2014154761A1
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WO
WIPO (PCT)
Prior art keywords
membrane
suction
medium
rotatable
membrane medium
Prior art date
Application number
PCT/EP2014/056080
Other languages
German (de)
English (en)
Inventor
Franz Liebermann
Cornelis Johannes Maria Van Rijn
Original Assignee
Mst Microsieve Technologies Gmbh
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Mst Microsieve Technologies Gmbh filed Critical Mst Microsieve Technologies Gmbh
Priority to US14/779,809 priority Critical patent/US10391455B2/en
Priority to EP14714656.7A priority patent/EP2978519B1/fr
Priority to ES14714656T priority patent/ES2955330T3/es
Publication of WO2014154761A1 publication Critical patent/WO2014154761A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/16—Rotary, reciprocated or vibrated modules
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D33/00—Filters with filtering elements which move during the filtering operation
    • B01D33/15—Filters with filtering elements which move during the filtering operation with rotary plane filtering surfaces
    • B01D33/21—Filters with filtering elements which move during the filtering operation with rotary plane filtering surfaces with hollow filtering discs transversely mounted on a hollow rotary shaft
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D33/00—Filters with filtering elements which move during the filtering operation
    • B01D33/44—Regenerating the filter material in the filter
    • B01D33/48—Regenerating the filter material in the filter by flushing, e.g. counter-current air-bumps
    • B01D33/50—Regenerating the filter material in the filter by flushing, e.g. counter-current air-bumps with backwash arms, shoes or nozzles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D33/00—Filters with filtering elements which move during the filtering operation
    • B01D33/44—Regenerating the filter material in the filter
    • B01D33/48—Regenerating the filter material in the filter by flushing, e.g. counter-current air-bumps
    • B01D33/50—Regenerating the filter material in the filter by flushing, e.g. counter-current air-bumps with backwash arms, shoes or nozzles
    • B01D33/503—Regenerating the filter material in the filter by flushing, e.g. counter-current air-bumps with backwash arms, shoes or nozzles the backwash arms, shoes acting on the cake side
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/08—Prevention of membrane fouling or of concentration polarisation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/10—Specific supply elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/54—Modularity of membrane module elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2315/00—Details relating to the membrane module operation
    • B01D2315/02—Rotation or turning
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2315/00—Details relating to the membrane module operation
    • B01D2315/16—Diafiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/26—By suction
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D33/00—Filters with filtering elements which move during the filtering operation
    • B01D33/15—Filters with filtering elements which move during the filtering operation with rotary plane filtering surfaces
    • B01D33/21—Filters with filtering elements which move during the filtering operation with rotary plane filtering surfaces with hollow filtering discs transversely mounted on a hollow rotary shaft
    • B01D33/23—Construction of discs or component sectors thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/40—Mixing liquids with liquids; Emulsifying
    • B01F23/41—Emulsifying

Definitions

  • the invention relates to a device with at least one membrane medium in a container, which can be used in the same construction both for filtration and for emulsification.
  • Filtration of liquids is typically the separation of unwanted particles from an unfiltered substance, e.g. B. from liquids, gases or suspensions, the so-called unfiltered, to produce two phases: a filtered, purified
  • particles present in the unfiltered solution also referred to as feed liquid, tend to accumulate on one or more areas of the filter medium surface, e.g. B. the membrane or Mikrosiebober arrangement to accumulate in the concentrate or retentate phase, d. H. that side of the filter medium or microsieve facing the unfiltered material.
  • Membrane or microsieve surface is thus gradually forming a cake or a
  • Microsieves are defined as very flat filtration membranes with high porosities (> 20%) and / or with pores with a pore channel length less than ten times or less than three times the pore diameter.
  • Backwashing takes place in this case after the filtration process.
  • Backwashing with short toiletriesst Schemeen so a reversal of the flow direction through the membrane by applying a negative TMD during the filtering process, ie without the termination, is also known.
  • Such backwashing methods are characterized by a relatively complicated structure and have only limited cleaning effect on membrane or Mikrosiebober inhabit. The effectiveness of these backflushing methods is limited by (1) rather low backwashing frequencies (1-60 times per hour) and (2) large distances between the location of triggering the backwash strokes and the
  • Membrane surfaces especially in industrial plants. The latter can either result in undesirable hammer blows or delays.
  • One known method of cross-flow filtration is the rotation of filter discs during filtration to reduce the formation of a cover layer by application of shear forces on the membrane or microsieve surface.
  • Examples of such filter systems are characterized by the stacking of filter discs with central bores, which are mounted on single or multiple hollow shafts. The filter disc stack is rotated about its axis.
  • Rotation speeds are often unable to remove particles from the pores of the filter medium as shown in FIG. Blocked pores can then only be opened by reversing the flow direction.
  • Airflow to be separated is achieved by a two-stage filter system in which mesh is stretched on rotating filter drums or discs.
  • mesh sizes which are typically in a range between 20 and 80 mesh (1.2 - 0.3 mm hole size).
  • the invention described herein is preferably for membrane filtration of liquids with micro, ultra and nano-filtration membranes having a mean pore size between 5 microns to 0.5 nanometers and, for example, for protein fractionation, beer clarification or sterile filtration of products from the
  • Process is in the present invention is not the classical backwashing but high-frequency flow reversal, also referred to as "rapid flow reversal".
  • the object of this invention is to enable the filtration efficiency of filter devices with, in particular, rotating filter media or micro-sieves in an economically feasible, technically innovative and scalable manner.
  • Unfiltratseite generate, although all substances that limit the filtration performance or prevent are on the unfiltrate facing membrane surface or in the pores. Thus, the individual pore is freed for a short time from a topcoat, which can then grow back immediately.
  • a thin horizontally stretched plastic film analogous to a biofilm or a cover layer into which an air hose from below by applying an overpressure pulse an opening (pore) beaten (analogous to a backwash pulse)
  • this opening closes after the pressure pulse, and the film (biofilm or cover layer) settles on the tube opening (pore) and clogs it again when pressure is applied from the top of the film.
  • the high-frequency flow reversal according to the invention starts on the membrane surface facing the unfiltered material, directly there where these layers form. As a result, these non-permeating substances, which are the cause of
  • Re-pulsation in the high-frequency flow reversal the covering layer forming substances removed by the suction slots of the membrane surface and transported away, not only pushed out of the pores.
  • the subject of this invention is the high-frequency flow reversal by means of a squeegee or a nozzle plate, which causes a short reversal of the flow direction during the
  • Membrane medium also as a membrane or in the application of filtration filter medium
  • the squeegee or nozzle plate generates a negative relative pressure in at least the same height as the transmembrane pressure applied during the filtration.
  • the high-frequency flow reversal typically occurs at frequencies between 1 and 100 Hz. High-frequency flow reversal is always necessary where high-performance filters with particularly efficient membrane layers are used
  • the invention makes it possible to reduce the loss of filtrate to a minimum, because the volume of liquid required to clean the membrane surface due to high-frequency flow reversal decreases with decreasing distance between suction slot and membrane surface with the third power. This possibility is given with none of today known backwash or back pulse systems.
  • the device according to the invention is suitable both for micro-, ultra- or nanofiltration (ie for pore sizes between 0.5 nm and 5 ⁇ m) and for the emulsification of liquids. It has at least one rotatable membrane medium with a filtrate / permeate side (in the case of filtration processes) or a side facing a disperse phase (at
  • Emulsion processes and a concentrate / retentate side (in the case of filtration) or of a side which faces a coherent phase (during emulsification).
  • the membrane medium is rotatable in a container.
  • the container has at least one feed for a non-filtrate or the coherent phase, at least one overflow for a non-filtrate or an emulsion and at least one rotatable channel for filtrate / permeate discharge or inflow of the disperse phase and a suction device.
  • a negative pressure generated By means of the suction device is on portions of the at least one rotatable membrane medium in the container, a negative pressure generated.
  • the negative pressure can be generated in small time intervals, wherein the negative pressure is preferably applied at intervals.
  • Provided is the application of a negative pressure with a frequency of 1-100 Hz. It is applied to an unfiltrate side or the coherent phase side facing.
  • Suction device has at least one parallel to the rotatable membrane medium arranged squeegee or nozzle plate or is such. It is mounted at a distance of less than 0.1-10 mm from the membrane medium. Preferably, the distance is less than 1 mm. In this way, a surface of the membrane medium can be cleaned from non-permeating substances accumulated on the nonfiltrate side during a filtration process, or, on the side facing the coherent phase, during an emulsification process, droplet formation of the disperse phase emerging from a membrane surface can be conveyed.
  • filtration performance can be optimized by continuously cleaning the filter medium or microsieve during the filtration of contaminants which may accumulate on the filter surface or membrane. This cleaning is accomplished during the filtration process by one or more nozzles or suction pads that locally exert a negative transmembrane pressure (TMD) on the membrane surfaces, which may also be referred to as filtering filtrate / permeate through the membrane or microsieve surfaces into the feed side of the filter housing ,
  • TMD negative transmembrane pressure
  • Flow reversal is called, at higher frequencies with very low filtrate / permeate volumes and very close to the membrane or Mikrosiebober formula, ie the place of the top layer formation carried out, whereby the filtration performance can be increased sustainably.
  • a filter device consisting of at least one filter medium 3, z. B. a microsieve, a filter housing and means for rotating the filter medium 3 in the filter housing, see Fig. 2, the filter medium during the filtration process with short periods of negative TMDs acted upon in the following manner.
  • a nozzle plate or squeegee 11 is mounted at a distance 9 of less than 1 mm to 5 mm from the rotating filter medium 3.
  • the holder of the squeegee or nozzle plate 7 is designated.
  • the nozzle plate or squeegee 11 is operated with a negative relative pressure or suction with respect to the TMD and thereby sucks the concentrate or retentate fluid over the membrane or microsieve surface. Since the nozzle or squeegee 11 is in the vicinity of the filter medium 3 or microsieve, also particles and covering layer components are sucked with the adsorbed liquid 6 in the nozzle or squeegee 11, and thus a locally efficient cleaning 10 of the
  • the nozzle or squeegee 11 is preferably mounted so that during a full rotation of the filter medium 3, is sucked over the entire effective area of the filter medium 3 to suck the entirety of the accumulated on the filter medium 3 particles and cover layers via the nozzle or suction bar 11.
  • the negative pressure which the nozzles or suction strips 11 exert locally on the filter medium 3 should be greater than the TMD.
  • a high flow resistance is created between the non-filtrate side and the suction strip 11. In this way, a sufficient negative pressure or suction pressure can be maintained.
  • the squeegee 11 near the filter medium will preferably be in the form of a flight (see Fig. 3, see reference numeral 12) to provide more laminar flow and / or turbulence and to provide improved suction.
  • the squeegee or nozzle plate 11 have at least one nozzle or slot, also referred to as suction slot 8, on which or which therefore in the squeegee or
  • Nozzle plate 11 is mounted parallel to the filter medium 3.
  • the nozzle or slot 8 should be placed as close as possible to this filter medium 3.
  • this distance 9 is less than 1 mm, and in particular the distance is between 0.05 and 0.25 mm. With a distance of less than z. B. 0.25 mm, a very good suction performance was achieved in experiments. The required liquid 6 flowing through the slot 8 is small.
  • the squeegee or nozzle plate 11 has a total width of a few mm to a few cm parallel to the filter medium 3.
  • Filter medium 3 is better transmitted in this way.
  • the total width of the squeegee or nozzle plate is about 10 times the distance of the squeegee or nozzle plate from the membrane medium - here the filter medium. It can be seen that the total width of the squeegee or nozzle plate depends on the total width of the filter medium to be cleaned. For filter media with large diameters, it may be necessary to provide several suction bars or nozzle plates side by side per filter medium. A squeegee or nozzle plate, which is at least five times wider than its distance from the diaphragm, turned out to be particularly effective.
  • the filter medium is sunk with a depth between 10 and 500 ⁇ in a filter support, preferably at a depth between 50 and 200 ⁇ .
  • the suction strips 11 or the slot-shaped nozzles 8 radially with respect to a filter medium 3, z. B. a round filter or Mikrosiebsay, and arranged perpendicular to the axis of rotation.
  • the width of the slot 8 should not be too low to
  • the width of the slot 8 should not be too large, since then the flow resistance between the squeegee and the filter medium is smaller.
  • the slot 8 will have a width between 50 ⁇ and 10 mm, and preferably between 200 ⁇ and 1 mm.
  • the parallel suction strip or nozzle plate 11 then has a width of a few millimeters to a few centimeters and is thus always wider than the width of the slot 8.
  • the total width of the suction / nozzle plate 11 is at least 10 times the width of a suction slot. 8 In the embodiment of Figures 2 and 3, the holder 7, the width of the suction slot 8 before.
  • the suction of the cover layer which is then removed by the holder 7 in the presented embodiment.
  • the suction strip 11 is wider than the suction slot 8. It ensures high shear forces; Accordingly, their distance from the filter medium 3 is set as low as possible.
  • a reverse flow generated by the application of a relative negative pressure, sufficient to remove the particles that are pressed by the TMD on the filter medium 3 or microsieve, by the nozzles or squeegee according fiction.
  • a targeted local vacuum 10 to 500 millibars is generated in this way. There is no need to do that
  • Essential for this invention is that the locally applied vacuum on the non-filtrate or concentrate or Retentatseite 1 through slots 8 (nozzles) is exerted in the squeegee or nozzle plate.
  • This pressure change, from relative overpressure, the TMD, to relative negative pressure on the surface of the filter medium 3, is preferably short-term and occurs, for example, several times within one second.
  • These pressure change phases consisting of TMD negative pressure TMD can be done very fast, short and in frequent sequences.
  • filtration performance may be dependent upon the nature of the unfiltered filtrate, the filtration device, the speed, the selected filter media 3, etc. depend. Accordingly, one skilled in the art will be able to understand the invention as a relative indication and take the necessary measures to adapt the invention to its needs and conditions. Thus, for example, attempts by the Applicant have improved the filtration performance by 1.5 to 60 times in comparison to
  • the filter medium 3 was set at an average speed between 1 and 100 Hz and the duration of the locally applied vacuum was applied periodically and for less than 1% of the total spin time. During the remaining rotation time (> 99%), the thus purified local filter medium contributes to the operational performance of the filtration process.
  • FIG. 6 shows an overview of the structure of a larger system of only two plug-together basic elements with central bore, which are stacked on a rotatable hollow shaft 19 and sealed with a cover 50 via tie rods 51.
  • the two basic elements are the interior and on the
  • FIG. 6 Overview drawing (Fig. 6) not visible rotating diaphragm support member (Fig. 7) and visible in Fig. 6 static pulse suction element (pulse-suction element), which also has membrane protection function.
  • the overall device in Fig. 6 is designated by the reference numeral 18.
  • the pulse suction element is designated by the reference numeral 37 and described in more detail in FIG. 9.
  • the two basic elements, membrane support element 60 (see FIG. 7) and pulse suction element 37 (see FIG. 9), are stacked alternately on a rotatable hollow shaft 19 (see FIG. 10) and fixed by tie rods (51), in particular four tie rods.
  • the membrane support member 60 (see Fig. 7) is rotatable. It rotates during operation. On it is the membrane medium, z. As the filter membrane or a membrane through which emulsification is carried out, supported.
  • the membrane medium is not shown in the representation of FIGS. 7 and 8.
  • the membrane support element 60 is characterized by a central bore 20 and filigree membrane support walls 21 with wall thicknesses between 0.1 mm and 1 mm, the filtrate / permeate flow through openings 22 in the cylindrical wall of the central bore 20 in the hollow shaft 19 (see Fig. 10) in Derive center.
  • the membrane support walls 21 are arranged at a distance 23 (see FIG. 8) between 0.1 cm and 10 cm.
  • membrane support member 60 and membrane medium or membrane disc ring are also called membrane disc in the present case.
  • the membrane medium for. As a membrane, between the inner outer edge, indicated by the outer sealing ring 29, and the outer inner edge, indicated by the inner sealing ring 30, the membrane support member 60, which are arranged flat to the membrane support walls 21, via a respective flat ring (inside and outside ) is fastened to the membrane support element 60 and sealed by an O-ring (inside and outside).
  • the membrane support member 60 made of glass and with a
  • Microsieve membrane are tightly connected by anodic bonding and thus sealed, eliminating further seals.
  • Membrane support members 60 to the axis of rotation symmetrical collar 31, at the outer end of these collapsed and sealed by an O-ring 32 against the filtrate channel which passes through the central bore 20.
  • Embodiment on a hollow shaft 19 are completely dispensed with.
  • the pulse sogelement 37 (FIG. 9) is static, ie it is not rotatable. It has a slightly larger central bore 33 than the membrane support element 60 (see Fig. 7 and 8) and engages around the circumference of the rotating diaphragm support member 60 to provide the necessary for inflow, overflow and suction of the unfiltered diameter, which depends on the operation and type of liquid to be filtered, provide. It also serves as
  • Protective hood for the membrane medium as a membrane has at the outer edge of several holes 34, typically 2 - 50 holes, for the inflow of the unfiltered.
  • Further bores 35 which are connected to the suction slots 36 via transverse bores 35a, provide for withdrawal of cover layers forming on the membrane surface via the suction slots 36.
  • the suction effect is generated via one or more pumps (not shown) arranged on the exit side of the bores 35 ,
  • These suction slots 36 are used for high-frequency flow reversal, and the number of holes 35 and 35a depends on the number of suction slots.
  • the suction slots 36 are radially disposed at 90 ° to the central bore 33 and are located at a distance of 1mm to 0.01mm parallel to the membrane surfaces.
  • the pulse suction element 37 is likewise constructed in the same way with respect to the central axis; so there are holes 34, 35, suction slots 36 and suction strips 38 both on the front 39 and also on the back 40 of the Pulsgsogelements 37.
  • Several pulse Suck elements 37 can be plugged together over the outer edge. in the
  • a Impulsgsogelements 37 is a groove 41, in which an O-ring can be placed and plugged together with the adjacent pulse Suction element, etc.
  • the hollow shaft 19 in Fig. 10 is characterized by holes 42 in the tube wall for the Filtratab Gustav and a driver 43 for the transmission of rotation to the membrane discs.
  • a driver 43 for the transmission of rotation to the membrane discs.
  • membrane support element with built-membrane medium z. B. the membrane ring described above.
  • the counterpart to the driver 43 is the recess 26 in the membrane support member 60.
  • the hollow shaft 19 is rotatable or is rotated during operation.
  • the dogs 43 engage in the indentations 26 of each membrane support member 60 and also put them in rotation.
  • Carrier 43 drag the membrane support elements 60 so to speak.
  • the invention can be operated in accordance with the invention in the reverse direction to produce emulsions with the same structure previously described by means of filtration.
  • the object of this invention is to improve the emulsification efficiency of
  • the disperse phase is filled via the hollow shaft 147 (see also FIG. 10) into the membrane support elements 144 (see also FIGS. 7 and 8).
  • a centrifugal force is formed, which continuously disperses the disperse phase through the pores of the membrane medium, shown here in the form of
  • Membrane discs 146 preferably microsieve discs (with radially in the direction
  • Membrane outer edge of decreasing pore diameters in order to compensate for the increasing in rotation of the membrane radially in the direction of the outer membrane edge pressures) through, in the pressureless coherent (continuous) phase suppressed.
  • Thin suction slots 136 with a width between 0.2 mm and 10 mm, in particular 0.5 and 2 mm, are mounted in the suction bars 138.
  • Membrane pores are exposed, pressed directly onto the membrane surface.
  • the application of a suction concentrated on a small segment of the rotating membrane surface and created by the static suction slots 136 on the membrane surface causes droplets of the dispersed phase forming on the membrane surface shortly after emerging from the membrane pores and before longer necks can form
  • Raised membrane surface there exposed to much higher shear forces, separated from the necks and pulled into the suction slots. This separation is preferably carried out in short periods of 1 - 100 Hz.
  • the resulting emulsion is withdrawn by means of a pump via the suction pipes 135.
  • the size of the drops and the size of the droplet size distribution of the disperse phase in the emulsion depends on the pore diameter of the membrane, rotational speed, number of suction bars and the applied suction (power of the suction pump).
  • the feed channel 148 serves for the continuous charging of the emulsifying device according to the invention the coherent phase.
  • the coherent phase is passed through the inlet channel 148 at pressures lower than that produced by centrifugal force at the membrane surfaces
  • Example 1 Filtration of skimmed milk: A microsieve (filter medium) with a pore size of 0.9 microns and a membrane thickness of about 1 micron and an open area of> 20% is placed in a rotatable disc, the filter carrier, at a distance of about 5 cm from the axis of rotation.
  • the filter container was filled with skim milk at 18-23 ° C and a constant TMD of 0.1 bar was set while rotating the disc with the filter medium at a constant rate of 20 cycles per second.
  • the initial filtration efficiency or flux was around 8,000 1 / m / h, but dropped to less than 500 l / m / h within a few seconds.
  • Nozzle plate used from the beginning, could be stable over 4 - 6 hours
  • the slot here has a width of 0.5 mm and a distance of about 500 ⁇ compared to the filter medium.
  • the peripheral speed is 2 ⁇ 5 cm and the effective filtration time is about 99.7%.
  • Example 2 Whole milk: Whole milk was filtered with 3.6% milk fat at 50 ° C with the inventive device described above and a microsieve filter medium with a pore diameter of 0.9 microns. At rotational speeds of 20 - 30
  • Example 3 Beer Filtration: Here a microsieve (filter medium) with a pore size of 0.6 microns is mounted in a rotatable disc about 5 cm from the axis of rotation.
  • the filter container was filled with unfiltered beer at 5 ° C and set a constant TMD of 0.1 bar.
  • the rotation of the disk with the filter medium was set at a constant speed of 10 cycles per second. The initial one
  • the slot here has a width of 0.8 mm and a distance of about 500 ⁇ compared to the filter medium.
  • the peripheral speed is 2 ⁇ 5 cm and the effective
  • Filtration time is about 99.5%.
  • Example 4 Emulsification: It is known that ceramic membranes are used extensively for
  • Emulsification applications have been studied with a non-rotating membrane device.
  • Typical dispersion phase flows of an oil in the preparation of an oil-in-water emulsion using a ceramic membrane with a medium
  • Pore size of 0.8 microns are 30-100 1 / m / h at an operating pressure of 3-10 bar.
  • the average emulsion droplet size is then typically a few microns with a wide droplet size distribution.
  • Figure 4 shows the flux when the nozzle or squeegee is operated and locally a reverse flow, according to the invention, as a function of the suction pressure (or energy) generated across the microsieve surface to remove particles and deposits.
  • an average beer filtration capacity of about 6,000 1 / m / h was measured (at TMD of 0.1 bar and 5 ° C) maintained for more than 16 hours.
  • FIG. 5 shows a rotary filtration device 81 in which a plurality of parallel micro-sieves rotate 82 equipped with integrated nozzle or squeegee 83, with inlet, overflow and Filtratablauf 84, 85 to collect the filtrate 86. It can be seen that the suction device has various suction extensions, which extend between the microsieves. It is periodically, with each revolution, the cover layer rich
  • the graph shows how fast the filtration performance collapses and how efficiently the
  • the invention may be used in a normal (non-rotating, also referred to as fixed) filter system where a plate may be provided with a number of slots which can be movably arranged with respect to the filter medium.
  • Figure 1 A cross-section in a schematic representation through a microsieve during filtration. Shown is a standard situation, as it already results after a short filtration time. It has built up a filter cake, a Deckschreib, on the filter medium, which blocks the pores.
  • FIG. 2 a schematic sectional view of the invention. It becomes clear as in
  • FIG. 3 an alternative embodiment of the invention
  • FIG. 4 shows a flux in a filter device according to the invention
  • FIG. 5 shows a further embodiment of the invention in the form of a rotating, horizontally arranged filter medium stack and a correspondingly designed suction device
  • Figure 6 an embodiment of the scaling of the invention constructed of two multipliable and pluggable basic elements in perspective view
  • FIG. 7 shows the rotatable membrane support element in plan view (left), in section (center) and in perspective (right);
  • FIG. 8 the membrane support element with filigree support walls arranged in the form of a circle involute
  • FIG. 9 the static repulsive pulse and membrane protection element in top view (left),
  • FIG. 10 shows a rotatable hollow shaft as the filtrate / permeate discharge channel
  • Embodiment of an emulsification device in plan view
  • FIG. 12 the emulsifying device of FIG. 11 in cross section
  • FIG. 13 a diagram representing the filtration flux over the time of two different test fluids and as a function of the pump power.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

La présente invention concerne un dispositif de micro-, ultra- ou nanofiltration et/ou d'émulsification de liquides. Le dispositif possède au moins un moyen formant membrane rotatif qui comprend un côté filtrat/perméat ou un côté tourné vers une phase dispersée et un côté concentré/rétentat ou un côté tourné vers une phase cohérente et qui peut tourner dans un récipient comportant au moins une arrivée pour un liquide non filtré ou pour la phase cohérente, au moins un trop-plein pour un liquide non filtré ou pour une émulsion, et au moins un conduit rotatif pour l'évacuation du filtrat/perméat ou l'arrivée de la phase dispersée, et un dispositif d'aspiration, en particulier sous la forme d'une rampe d'aspiration ou d'une plaque à buses, servant à générer un vide dans des zones partielles du ou des moyens formant membranes rotatifs dans le récipient pendant de courtes périodes à une fréquence de 1 à 100 Hz, sur un côté liquide non filtré ou tourné vers la phase cohérente. Le dispositif d'aspiration comporte au moins une rampe d'aspiration ou une plaque à buses disposée parallèlement au moyen formant membrane rotatif, ou il s'agit d'un dispositif d'aspiration qui est monté avec un écartement de moins de 0,1 à 10 mm par rapport au moyen formant membrane et qui nettoie ainsi une surface du moyen formant membrane des substances non perméantes accumulées sur le côté liquide non filtré pendant une opération de filtration ou qui favorise une formation de gouttes de la phase dispersée sortant d'une surface de la membrane sur le côté tourné vers la phase cohérente pendant une opération d'émulsification. L'invention concerne en outre des utilisations de ce dispositif.
PCT/EP2014/056080 2013-03-26 2014-03-26 Dispositif de filtration et d'émulsification WO2014154761A1 (fr)

Priority Applications (3)

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US14/779,809 US10391455B2 (en) 2013-03-26 2014-03-26 Filtration and emulsification device
EP14714656.7A EP2978519B1 (fr) 2013-03-26 2014-03-26 Dispositif de filtration et d'émulsification
ES14714656T ES2955330T3 (es) 2013-03-26 2014-03-26 Dispositivo de filtración y emulsificación

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DE202013101302.1 2013-03-26
DE202013101302U DE202013101302U1 (de) 2013-03-26 2013-03-26 Filtrationsvorrichtung

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ES2955330T3 (es) 2023-11-30
US20160045871A1 (en) 2016-02-18
US10391455B2 (en) 2019-08-27
EP2978519A1 (fr) 2016-02-03
EP2978519C0 (fr) 2023-07-26
DE202013101302U1 (de) 2013-05-06
EP2978519B1 (fr) 2023-07-26

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